Chemical Properties of Tetradecane (CAS 629-59-4)

InChI

InChI=1S/C14H30/c1-3-5-7-9-11-13-14-12-10-8-6-4-2/h3-14H2,1-2H3

InChI Key

BGHCVCJVXZWKCC-UHFFFAOYSA-N

Formula

C14H30

SMILES

CCCCCCCCCCCCCC

Molecular Weight¹

198.39

CAS

629-59-4

Other Names

• n-tetradecane

• ω : Acentric Factor.
• α_p : Isobaric thermal expansion coefficient (1/K).
• Δ_cH°_gas : Standard gas enthalpy of combustion (kJ/mol).
• C_p,gas : Ideal gas heat capacity (J/mol×K).
• C_p,liquid : Liquid phase heat capacity (J/mol×K).
• μ : Dipole Moment (debye).
• η : Dynamic viscosity (Pa×s).
• Δ_fG° : Standard Gibbs free energy of formation (kJ/mol).
• Δ_fH°_gas : Enthalpy of formation at standard conditions (kJ/mol).
• Δ_fH°_liquid : Liquid phase enthalpy of formation at standard conditions (kJ/mol).
• Δ_fusH° : Enthalpy of fusion at standard conditions (kJ/mol).
• Δ_fusH : Enthalpy of fusion at a given temperature (kJ/mol).
• Δ_subH° : Enthalpy of sublimation at standard conditions (kJ/mol).
• Δ_vapH° : Enthalpy of vaporization at standard conditions (kJ/mol).
• Δ_vapH : Enthalpy of vaporization at a given temperature (kJ/mol).
• IE : Ionization energy (eV).
• log₁₀WS : Log10 of Water solubility in mol/l.
• logP_oct/wat : Octanol/Water partition coefficient.
• McVol : McGowan's characteristic volume (ml/mol).
• P_c : Critical Pressure (kPa).
• P_triple : Triple Point Pressure (kPa).
• P_vap : Vapor pressure (kPa).
• n₀ : Refractive Index.
• ρ_c : Critical density (kg/m³).
• ρ_l : Liquid Density (kg/m³).
• I_np : Non-polar retention indices.
• Δ_fusS : Entropy of fusion at a given temperature (J/mol×K).
• S°_gas : Molar entropy at standard conditions (J/mol×K).
• S°_liquid : Liquid phase molar entropy at standard conditions (J/mol×K).
• γ : Surface Tension (N/m).
• T_boil : Normal Boiling Point Temperature (K).
• T_boilr : Boiling point at reduced pressure (K).
• T_c : Critical Temperature (K).
• λ_gas : Gas thermal conductivity (W/m×K).
• λ_liquid : Liquid thermal conductivity (W/m×K).
• T_fus : Normal melting (fusion) point (K).
• T_fus(P) : Melting point (K).
• T_triple : Triple Point Temperature (K).
• U_Qi : UNIQUAC Qi Parameter.
• U_Ri : UNIQUAC Ri Parameter.
• V_c : Critical Volume (m³/kmol).
• V_COSTALD : COSTALD Characteristic Volume (m³/kmol).
• ω_SRK : SRK acentric factor.
• Z_c : Critical Compressibility.
• Z_ra : Rackett Parameter.
• ¹: Molecular weight from the IUPAC atomic weights tables.

Contents

1. Physical Properties
2. Temperature Dependent Properties
3. Pressure Dependent Properties
4. Datasets
5. Correlations
6. Similar Compounds
7. Mixtures
8. Sources

Physical Properties

Property	Value	Unit	Source
ω	[0.5810; 0.6797]
ω	0.6790		PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
ω	0.6797		Passut and Danner (1973), critical constants and acentric factors Compiled value
ω	0.6440		ChemSep v8.3 pure component data Compiled value
ω	0.5810		KDB
ΔcH°gas	-9393.50 ± 1.60	kJ/mol	NIST
μ	0.00	debye	ChemSep v8.3 pure component data Compiled value
ΔfG°	[65.99; 66.86]	kJ/mol
ΔfG°	65.99	kJ/mol	ChemSep v8.3 pure component data Compiled value
ΔfG°	66.86	kJ/mol	KDB
ΔfH°gas	[-332.44; -332.10]	kJ/mol
ΔfH°gas	-332.44	kJ/mol	ChemSep v8.3 pure component data Compiled value
ΔfH°gas	-332.30	kJ/mol	KDB
ΔfH°gas	-332.10 ± 1.80	kJ/mol	NIST
ΔfH°liquid	-403.30 ± 1.80	kJ/mol	NIST
ΔfusH°	32.02	kJ/mol	Joback Calculated Property
ΔsubH°	117.60	kJ/mol	NIST
ΔvapH°	[71.10; 72.10]	kJ/mol
ΔvapH°	71.30	kJ/mol	NIST
ΔvapH°	71.60 ± 1.30	kJ/mol	NIST
ΔvapH°	72.10	kJ/mol	NIST
ΔvapH°	72.00 ± 2.40	kJ/mol	NIST
ΔvapH°	71.20	kJ/mol	NIST
ΔvapH°	71.40	kJ/mol	NIST
ΔvapH°	71.70	kJ/mol	NIST
ΔvapH°	71.80 ± 0.60	kJ/mol	NIST
ΔvapH°	71.10 ± 0.40	kJ/mol	NIST
ΔvapH°	71.70	kJ/mol	NIST
IE	9.74	eV	Relay (1.0) Calculated Property
log10WS	[-7.96; -7.96]
log10WS	-7.96		Aq. Solubility Prediction
log10WS	-7.96		Estimated Solubility
logPoct/wat	5.707		Crippen Calculated Property
McVol	208.120	ml/mol	McGowan Calculated Property
Pc	[1438.00; 1620.27]	kPa
Pc	1570.00	kPa	IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 2 Compiled value
Pc	1572.56	kPa	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Pc	1620.27	kPa	Passut and Danner (1973), critical constants and acentric factors Compiled value
Pc	1570.00	kPa	ChemSep v8.3 pure component data Compiled value
Pc	1570.00	kPa	KDB
Pc	1600.00 ± 200.00	kPa	NIST
Pc	1573.00 ± 20.00	kPa	NIST
Pc	1440.00	kPa	NIST
Pc	1438.00 ± 68.94	kPa	NIST
Ptriple	2.53e-04	kPa	ChemSep v8.3 pure component data Compiled value
ρc	[218.23; 222.19]	kg/m3
ρc	218.23 ± 39.68	kg/m3	NIST
ρc	222.19 ± 5.95	kg/m3	NIST
Inp	[236.21; 239.35]
Inp	236.21		NIST
Inp	239.35		NIST
S°gas	700.40	J/mol×K	NIST
S°liquid	[555.43; 562.30]	J/mol×K
S°liquid	555.43	J/mol×K	NIST
S°liquid	562.30	J/mol×K	NIST
Tboil	[510.00; 528.00]	K
Tboil	526.76	K	ChemSep v8.3 pure component data Compiled value
Tboil	526.73	K	KDB
Tboil	526.90	K	NIST
Tboil	524.15 ± 0.60	K	NIST
Tboil	525.15 ± 0.40	K	NIST
Tboil	526.40 ± 0.30	K	NIST
Tboil	528.00 ± 2.00	K	NIST
Tboil	526.04 ± 0.30	K	NIST
Tboil	512.00 ± 3.00	K	NIST
Tboil	Outlier 510.00 ± 6.00	K	NIST
Tboil	525.70 ± 3.00	K	NIST
Tc	[691.20; 696.90]	K
Tc	693.00	K	IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 2 Compiled value
Tc	691.80	K	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Tc	691.87	K	Passut and Danner (1973), critical constants and acentric factors Compiled value
Tc	693.00	K	ChemSep v8.3 pure component data Compiled value
Tc	693.00	K	KDB
Tc	693.00 ± 2.00	K	NIST
Tc	693.00 ± 1.20	K	NIST
Tc	691.80 ± 0.70	K	NIST
Tc	693.00 ± 1.20	K	NIST
Tc	692.30	K	NIST
Tc	691.20 ± 1.50	K	NIST
Tc	694.00	K	NIST
Tc	692.80 ± 1.00	K	NIST
Tc	692.80 ± 1.00	K	NIST
Tc	Outlier 696.90 ± 2.00	K	NIST
Tc	694.15 ± 1.00	K	NIST
Tfus	[251.00; 279.40]	K
Tfus	279.40	K	Experimental measurements and thermodynamic modeling of wax disappearance temperature for the binary systems n-C14H30 + n- C16H34, n-C16H34 + n-C18H38 and n-C11H24 + n-C18H38
Tfus	278.90	K	Determination of thermophysical properties of cyclopentane hydrate using a stirred calorimetric cell
Tfus	279.05	K	Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value
Tfus	279.01	K	ChemSep v8.3 pure component data Compiled value
Tfus	279.01	K	KDB
Tfus	278.98	K	Aq. Solubility Prediction
Tfus	278.99 ± 0.05	K	NIST
Tfus	278.97 ± 0.02	K	NIST
Tfus	279.00 ± 0.20	K	NIST
Tfus	279.00 ± 0.20	K	NIST
Tfus	279.00 ± 0.20	K	NIST
Tfus	279.00 ± 0.20	K	NIST
Tfus	279.00 ± 0.20	K	NIST
Tfus	279.15 ± 0.50	K	NIST
Tfus	278.70 ± 2.00	K	NIST
Tfus	278.99 ± 0.30	K	NIST
Tfus	279.00 ± 0.30	K	NIST
Tfus	278.40 ± 0.30	K	NIST
Tfus	Outlier 251.00 ± 5.00	K	NIST
Tfus	279.00 ± 0.01	K	NIST
Tfus	279.00 ± 0.01	K	NIST
Tfus	279.01 ± 0.01	K	NIST
Tfus	278.90 ± 0.30	K	NIST
Tfus	278.90 ± 0.20	K	NIST
Tfus	278.92 ± 0.20	K	NIST
Tfus	279.00 ± 0.05	K	NIST
Tfus	279.01 ± 0.01	K	NIST
Tfus	277.85 ± 1.00	K	NIST
Tfus	279.01 ± 0.02	K	NIST
Tfus	279.20 ± 1.00	K	NIST
Tfus	279.20 ± 1.00	K	NIST
Tfus	278.80 ± 1.00	K	NIST
Tfus	277.40 ± 2.00	K	NIST
Tfus	278.70 ± 0.70	K	NIST
Tfus	278.00 ± 2.00	K	NIST
Tfus	278.60 ± 2.00	K	NIST
Tfus	277.70 ± 2.00	K	NIST
Tfus	277.70 ± 2.00	K	NIST
Ttriple	[279.01; 279.02]	K
Ttriple	279.01	K	ChemSep v8.3 pure component data Compiled value
Ttriple	279.02 ± 0.05	K	NIST
Ttriple	279.02 ± 0.02	K	NIST
Ttriple	279.02 ± 0.20	K	NIST
Ttriple	279.01 ± 0.20	K	NIST
Ttriple	279.02 ± 0.02	K	NIST
UQi	8.18		ChemSep v8.3 pure component data Compiled value
URi	9.89		ChemSep v8.3 pure component data Compiled value
Vc	[0.894; 0.894]	m3/kmol
Vc	0.894	m3/kmol	IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 2 Compiled value
Vc	Outlier 0.894	m3/kmol	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Vc	0.894	m3/kmol	ChemSep v8.3 pure component data Compiled value
Vc	0.894	m3/kmol	KDB
Vc	0.894	m3/kmol	NIST
VCOSTALD	0.90	m3/kmol	Hankinson and Thomson (1979), COSTALD parameters Compiled value
ωSRK	0.68		Hankinson and Thomson (1979), COSTALD parameters Compiled value
Zc	[0.2435940; 0.2440000]
Zc	0.2440000		IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 2 Compiled value
Zc	0.2440000		ChemSep v8.3 pure component data Compiled value
Zc	0.2435940		KDB
Zra	[0.23; 0.24]
Zra	0.24		Hankinson and Thomson (1979), COSTALD parameters Compiled value
Zra	0.23		ChemSep v8.3 pure component data Compiled value

Temperature Dependent Properties

Property	Value	Unit	Temperature (K)	Source
Cp,liquid	[433.53; 438.44]	J/mol×K	[290.60; 298.15]
Cp,liquid	434.30	J/mol×K	290.60	NIST
Cp,liquid	435.10	J/mol×K	296.20	NIST
Cp,liquid	436.00	J/mol×K	298.00	NIST
Cp,liquid	434.20	J/mol×K	298.15	NIST
Cp,liquid	438.01	J/mol×K	298.15	NIST
Cp,liquid	434.16	J/mol×K	298.15	NIST
Cp,liquid	433.98	J/mol×K	298.15	NIST
Cp,liquid	433.53	J/mol×K	298.15	NIST
Cp,liquid	438.28	J/mol×K	298.15	NIST
Cp,liquid	434.20	J/mol×K	298.15	NIST
Cp,liquid	433.53	J/mol×K	298.15	NIST
Cp,liquid	436.40	J/mol×K	298.15	NIST
Cp,liquid	436.52	J/mol×K	298.15	NIST
Cp,liquid	436.91	J/mol×K	298.15	NIST
Cp,liquid	438.01	J/mol×K	298.15	NIST
Cp,liquid	438.44	J/mol×K	298.15	NIST
Cp,liquid	434.20	J/mol×K	298.15	NIST
η	[0.0015940; 0.0023460]	Pa×s	[293.15; 313.15]
η	0.0023460	Pa×s	293.15	Densities and Viscosities of Binary Mixtures of exo-Tetrahydrodicyclopentadiene with N-Undecane or N-Tetradecane at T = (293.15 to 313.15) K
η	0.0021070	Pa×s	298.15	Densities and Viscosities of Binary Mixtures of exo-Tetrahydrodicyclopentadiene with N-Undecane or N-Tetradecane at T = (293.15 to 313.15) K
η	0.0018970	Pa×s	303.15	Densities and Viscosities of Binary Mixtures of exo-Tetrahydrodicyclopentadiene with N-Undecane or N-Tetradecane at T = (293.15 to 313.15) K
η	0.0015940	Pa×s	313.15	Densities and Viscosities of Binary Mixtures of exo-Tetrahydrodicyclopentadiene with N-Undecane or N-Tetradecane at T = (293.15 to 313.15) K
ΔfusH	[42.70; 45.07]	kJ/mol	[278.30; 279.03]
ΔfusH	42.70	kJ/mol	278.30	NIST
ΔfusH	45.07	kJ/mol	279.00	NIST
ΔfusH	45.07	kJ/mol	279.00	NIST
ΔfusH	45.07	kJ/mol	279.03	NIST
ΔfusH	45.07	kJ/mol	279.03	NIST
ΔvapH	[47.61; 70.10]	kJ/mol	[313.00; 526.10]
ΔvapH	70.10	kJ/mol	313.00	NIST
ΔvapH	69.00	kJ/mol	324.00	NIST
ΔvapH	68.90	kJ/mol	328.00	NIST
ΔvapH	68.60	kJ/mol	329.00	NIST
ΔvapH	67.90	kJ/mol	334.00	NIST
ΔvapH	66.80	kJ/mol	344.00	NIST
ΔvapH	65.70	kJ/mol	359.00	NIST
ΔvapH	64.10	kJ/mol	369.00	NIST
ΔvapH	67.80	kJ/mol	373.00	NIST
ΔvapH	57.80	kJ/mol	448.50	NIST
ΔvapH	57.10	kJ/mol	480.50	NIST
ΔvapH	47.61	kJ/mol	526.10	KDB
Pvap	[4.27e-04; 50.70]	kPa	[283.15; 498.07]
Pvap	4.27e-04	kPa	283.15	Gas Saturation Vapor Pressure Measurements of Mononitrotoluene Isomers from (283.15 to 313.15) K
Pvap	1.21e-03	kPa	293.15	Gas Saturation Vapor Pressure Measurements of Mononitrotoluene Isomers from (283.15 to 313.15) K
Pvap	3.22e-03	kPa	303.15	Gas Saturation Vapor Pressure Measurements of Mononitrotoluene Isomers from (283.15 to 313.15) K
Pvap	8.10e-03	kPa	313.15	Gas Saturation Vapor Pressure Measurements of Mononitrotoluene Isomers from (283.15 to 313.15) K
Pvap	0.12	kPa	351.75	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.14	kPa	353.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.14	kPa	353.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.23	kPa	361.80	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.23	kPa	361.89	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.25	kPa	363.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.42	kPa	371.91	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.45	kPa	373.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.44	kPa	373.15	Isothermal Vapor Liquid Equilibria of n-Tetradecane + Ethyl Hexanoate, Ethyl Decanoate, and Ethyl Tetradecanoate
Pvap	0.45	kPa	373.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.72	kPa	381.93	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.72	kPa	382.07	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.75	kPa	383.15	Isothermal Vapor Liquid Equilibria of n-Tetradecane + Ethyl Hexanoate, Ethyl Decanoate, and Ethyl Tetradecanoate
Pvap	0.76	kPa	383.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	0.76	kPa	383.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	1.19	kPa	391.95	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	1.19	kPa	392.00	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	1.25	kPa	393.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	1.23	kPa	393.15	Isothermal Vapor Liquid Equilibria of n-Tetradecane + Ethyl Hexanoate, Ethyl Decanoate, and Ethyl Tetradecanoate
Pvap	1.25	kPa	393.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	1.95	kPa	402.74	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	1.95	kPa	403.15	Isothermal Vapor Liquid Equilibria of n-Tetradecane + Ethyl Hexanoate, Ethyl Decanoate, and Ethyl Tetradecanoate
Pvap	2.00	kPa	403.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	3.03	kPa	412.69	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	3.09	kPa	413.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	3.02	kPa	413.15	Isothermal Vapor Liquid Equilibria of n-Tetradecane + Ethyl Hexanoate, Ethyl Decanoate, and Ethyl Tetradecanoate
Pvap	3.09	kPa	413.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	4.54	kPa	422.55	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	4.64	kPa	423.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	4.65	kPa	423.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	4.54	kPa	423.15	Isothermal Vapor Liquid Equilibria of n-Tetradecane + Ethyl Hexanoate, Ethyl Decanoate, and Ethyl Tetradecanoate
Pvap	6.66	kPa	432.39	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	6.81	kPa	433.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	6.84	kPa	433.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	6.68	kPa	433.15	Isothermal Vapor Liquid Equilibria of n-Tetradecane + Ethyl Hexanoate, Ethyl Decanoate, and Ethyl Tetradecanoate
Pvap	9.46	kPa	442.49	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	9.78	kPa	443.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	9.63	kPa	443.15	Isothermal Vapor Liquid Equilibria of n-Tetradecane + Ethyl Hexanoate, Ethyl Decanoate, and Ethyl Tetradecanoate
Pvap	13.46	kPa	452.49	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	13.60	kPa	453.15	Isothermal Vapor Liquid Equilibria of n-Tetradecane + Ethyl Hexanoate, Ethyl Decanoate, and Ethyl Tetradecanoate
Pvap	13.75	kPa	453.15	Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
Pvap	40.00	kPa	489.17	Low-Pressure VLE Measurements and Thermodynamic Modeling, with PSRK and NRTL, of Binary 1-Alcohol + n-Alkane Systems
Pvap	40.04	kPa	489.26	Low-Pressure VLE Measurements and Thermodynamic Modeling, with PSRK and NRTL, of Binary 1-Alcohol + n-Alkane Systems
Pvap	42.42	kPa	491.29	Low-Pressure VLE Measurements and Thermodynamic Modeling, with PSRK and NRTL, of Binary 1-Alcohol + n-Alkane Systems
Pvap	43.80	kPa	492.53	Low-Pressure VLE Measurements and Thermodynamic Modeling, with PSRK and NRTL, of Binary 1-Alcohol + n-Alkane Systems
Pvap	46.96	kPa	495.18	Low-Pressure VLE Measurements and Thermodynamic Modeling, with PSRK and NRTL, of Binary 1-Alcohol + n-Alkane Systems
Pvap	48.13	kPa	496.08	Low-Pressure VLE Measurements and Thermodynamic Modeling, with PSRK and NRTL, of Binary 1-Alcohol + n-Alkane Systems
Pvap	50.50	kPa	497.96	Low-Pressure VLE Measurements and Thermodynamic Modeling, with PSRK and NRTL, of Binary 1-Alcohol + n-Alkane Systems
Pvap	50.70	kPa	498.07	Low-Pressure VLE Measurements and Thermodynamic Modeling, with PSRK and NRTL, of Binary 1-Alcohol + n-Alkane Systems
n0	[1.42360; 1.42910]		[293.10; 308.15]
n0	1.42910		293.10	Liquid liquid equilibria for n-alkanes (C12, C14, C17) + propylbenzene +NMP mixtures at temperatures between 298 and 328K
n0	1.42910		293.10	Extraction of pentylbenzene from high molar mass alkanes (C14 and C17) by N-methyl-2-pyrrolidone
n0	1.42890		293.10	Evaluation of [bmim][PF6] as an ionic solvent for the extraction of propylbenzene from aliphatic compounds
n0	1.42690		298.15	Liquid-Liquid Equilibria for Ternary Mixtures of gamma-Valerolactone + n-Tetradecane + (Butanoic Acid or Hexanoic Acid or Methyl Myristate) at 298.15 K
n0	1.42730		298.15	Measurement and Prediction of Excess Properties of Binary Mixtures Methyl Decanoate + an Even-Numbered n-Alkane (C6-C16) at 298.15 K
n0	1.42820		298.15	Density, Viscosity, Refractive Index, and Speed of Sound in the Binary Mixtures of Tri-n-butylamine + Triethylamine, + Tetrahydrofuran, + Tetradecane, + Tetrachloroethylene, + Pyridine, or + Trichloroethylene at (298.15, 303.15, and 308.15) K
n0	1.42600		303.15	Density, Viscosity, Refractive Index, and Speed of Sound in the Binary Mixtures of Tri-n-butylamine + Triethylamine, + Tetrahydrofuran, + Tetradecane, + Tetrachloroethylene, + Pyridine, or + Trichloroethylene at (298.15, 303.15, and 308.15) K
n0	1.42360		308.15	Density, Viscosity, Refractive Index, and Speed of Sound in the Binary Mixtures of Tri-n-butylamine + Triethylamine, + Tetrahydrofuran, + Tetradecane, + Tetrachloroethylene, + Pyridine, or + Trichloroethylene at (298.15, 303.15, and 308.15) K
ρl	[727.10; 767.00]	kg/m3	[293.00; 344.15]
ρl	763.00	kg/m3	293.00	KDB
ρl	767.00	kg/m3	293.15	Volume expansion prediction of supercritical CO 2 + crude oil
ρl	763.09	kg/m3	293.15	Excess Molar Volumes and Viscosities of Binary Systems of Butylcyclohexane with n-Alkanes (C7 to C14) at T = 293.15 K to 313.15 K
ρl	759.36	kg/m3	298.15	Excess Enthalpies of Binary Mixtures of 1-Hexene with Some n-Alkanes at 298.15 K
ρl	759.27	kg/m3	298.15	Thermodynamics of Mixtures Containing Aromatic Alcohols. 1. Liquid Liquid Equilibria for (Phenylmethanol + Alkane) Systems
ρl	759.38	kg/m3	298.15	Solubility behavior of .gamma.-valerolactone + n-tetradecane or diesel mixtures at different temperatures
ρl	760.20	kg/m3	298.15	Excess molar enthalpies of binary mixtures containing 2-decanone or dipentyl ether with long-chain n-alkanes at T = 298.15 K
ρl	759.19	kg/m3	298.15	Thermodynamics of mixtures containing amines. XI. Liquid + liquid equilibria and molar excess enthalpies at 298.15 K for N-methylaniline + hydrocarbon systems. Characterization in terms of DISQUAC and ERAS models
ρl	759.27	kg/m3	298.15	Liquid Liquid Equilibria for Systems Containing 4-Phenylbutan-2-one or Benzyl Ethanoate and Selected Alkanes
ρl	759.27	kg/m3	298.15	Liquid-Liquid Equilibria for 2-Phenylethan-1-ol + Alkane Systems
ρl	759.27	kg/m3	298.15	Liquid-liquid equilibria for benzaldehyde + n-alkane mixtures andcharacterization of benzaldehyde + hydrocarbon systems in terms of DISQUAC
ρl	759.27	kg/m3	298.15	Thermodynamics of Mixtures Containing Ethers. Part III. Liquid-Liquid Equilibria for 2,5,8,11-Tetraoxadodecane or 2,5,8,11,14-Pentaoxapentadecane + Selected N-Alkanes
ρl	759.27	kg/m3	298.15	Thermodynamics of aromatic polar compound (alkanone, alkanal or alkanoate) + hydrocarbon mixtures
ρl	759.27	kg/m3	298.15	Thermodynamics of Mixtures Containing a Very Strongly Polar Compound. 10. Liquid Liquid Equilibria for N,N-Dimethylacetamide + Selected Alkanes
ρl	759.27	kg/m3	298.15	Liquid liquid equilibria for acetophenone + n-alkane mixtures and characterization of acetophenone systems using DISQUAC
ρl	759.57	kg/m3	298.15	Excess Molar Volumes and Viscosities of Binary Systems of Butylcyclohexane with n-Alkanes (C7 to C14) at T = 293.15 K to 313.15 K
ρl	760.20	kg/m3	298.15	Excess Molar Enthalpies of Binary Systems of n-Valeric Anhydride or n-Hexanoic Anhydride with n-Dodecane, n-Tetradecane, or n-Hexadecane at 298.15 K
ρl	760.20	kg/m3	298.15	Excess Molar Enthalpies of Binary Systems of 2-Octanone or 3-Octanone with Dodecane, Tetradecane, or Hexadecane at 298.15 K
ρl	759.32	kg/m3	298.15	Thermodynamics of Mixtures Containing Amines. XV. Liquid Liquid Equilibria for Benzylamine + CH3(CH2)nCH3 (n = 8, 9, 10, 12, 14)
ρl	756.03	kg/m3	303.15	Excess Molar Volumes and Viscosities of Binary Systems of Butylcyclohexane with n-Alkanes (C7 to C14) at T = 293.15 K to 313.15 K
ρl	752.51	kg/m3	308.15	Excess Molar Volumes and Viscosities of Binary Systems of Butylcyclohexane with n-Alkanes (C7 to C14) at T = 293.15 K to 313.15 K
ρl	748.98	kg/m3	313.15	Excess Molar Volumes and Viscosities of Binary Systems of Butylcyclohexane with n-Alkanes (C7 to C14) at T = 293.15 K to 313.15 K
ρl	727.10	kg/m3	344.15	High-pressure densities and interfacial tensions of binary systems containing carbon dioxide + n-alkanes: (n-Dodecane, n-tridecane, n-tetradecane)
ΔfusS	[161.52; 161.52]	J/mol×K	[279.03; 279.03]
ΔfusS	161.52	J/mol×K	279.03	NIST
ΔfusS	161.52	J/mol×K	279.03	NIST
γ	[0.02; 0.03]	N/m	[293.20; 313.15]
γ	0.03	N/m	293.20	KDB
γ	0.03	N/m	294.60	Density, Viscosity, Speed of Sound, Bulk Modulus, Surface Tension, and Flash Point of Binary Mixtures of Butylbenzene + Linear Alkanes (n-Decane, n-Dodecane, n-Tetradecane, n-Hexadecane, or n-Heptadecane) at 0.1 MPa
γ	0.02	N/m	313.15	Interfacial tensions of binary mixtures of ethanol with octane, decane, dodecane, and tetradecane

Pressure Dependent Properties

Property	Value	Unit	Pressure (kPa)	Source
Tboilr	395.10	K	1.30	NIST
Tfus(P)	[279.20; 301.70]	K	[100.00; 100000.00]
Tfus(P)	279.20	K	100.00	Liquid solid equilibria under high pressure of tetradecane + pentadecane and tetradecane + hexadecane binary systems
Tfus(P)	284.20	K	20000.00	Liquid solid equilibria under high pressure of tetradecane + pentadecane and tetradecane + hexadecane binary systems
Tfus(P)	289.10	K	40000.00	Liquid solid equilibria under high pressure of tetradecane + pentadecane and tetradecane + hexadecane binary systems
Tfus(P)	293.80	K	60000.00	Liquid solid equilibria under high pressure of tetradecane + pentadecane and tetradecane + hexadecane binary systems
Tfus(P)	297.90	K	80000.00	Liquid solid equilibria under high pressure of tetradecane + pentadecane and tetradecane + hexadecane binary systems
Tfus(P)	301.70	K	100000.00	Liquid solid equilibria under high pressure of tetradecane + pentadecane and tetradecane + hexadecane binary systems

Datasets

1. Isobaric coefficient of expansion, 1/K (1)
2. Molar heat capacity at constant pressure, J/K/mol (1)
3. Viscosity, Pa*s (1)
4. Mass density, kg/m3 (5)

Isobaric coefficient of expansion, 1/K

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Isobaric coefficient of expansion, 1/K - Liquid
298.15	5000.00	0.0009
298.15	10000.00	0.0009
298.15	15000.00	0.0009
298.15	20000.00	0.0008
298.15	25000.00	0.0008
298.15	30000.00	0.0008
298.15	35000.00	0.0008
298.15	40000.00	0.0008
298.15	45000.00	0.0008
298.15	50000.00	0.0007
298.15	55000.00	0.0007
308.15	5000.00	0.0009
308.15	10000.00	0.0009
308.15	15000.00	0.0009
308.15	20000.00	0.0008
308.15	25000.00	0.0008
308.15	30000.00	0.0008
308.15	35000.00	0.0008
308.15	40000.00	0.0008
308.15	45000.00	0.0007
308.15	50000.00	0.0007
308.15	55000.00	0.0007
318.15	5000.00	0.0009
318.15	10000.00	0.0009
318.15	15000.00	0.0009
318.15	20000.00	0.0008
318.15	25000.00	0.0008
318.15	30000.00	0.0008
318.15	35000.00	0.0008
318.15	40000.00	0.0008
318.15	45000.00	0.0007
318.15	50000.00	0.0007
318.15	55000.00	0.0007
328.15	5000.00	0.0009
328.15	10000.00	0.0009
328.15	15000.00	0.0009
328.15	20000.00	0.0008
328.15	25000.00	0.0008
328.15	30000.00	0.0008
328.15	35000.00	0.0008
328.15	40000.00	0.0008
328.15	45000.00	0.0007
328.15	50000.00	0.0007
328.15	55000.00	0.0007
338.15	5000.00	0.0009
338.15	10000.00	0.0009
338.15	15000.00	0.0009
338.15	20000.00	0.0008
338.15	25000.00	0.0008
338.15	30000.00	0.0008
338.15	35000.00	0.0008
338.15	40000.00	0.0007
338.15	45000.00	0.0007
338.15	50000.00	0.0007
338.15	55000.00	0.0007
348.15	5000.00	0.0009
348.15	10000.00	0.0009
348.15	15000.00	0.0009
348.15	20000.00	0.0008
348.15	25000.00	0.0008
348.15	30000.00	0.0008
348.15	35000.00	0.0008
348.15	40000.00	0.0007
348.15	45000.00	0.0007
348.15	50000.00	0.0007
348.15	55000.00	0.0007
Reference

Molar heat capacity at constant pressure, J/K/mol

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Molar heat capacity at constant pressure, J/K/mol - Liquid
323.15	120.00	449.55
328.15	120.00	452.72
333.15	120.00	456.09
338.15	120.00	459.47
343.15	120.00	463.04
348.15	120.00	466.61
353.15	120.00	470.38
358.15	120.00	474.15
363.15	120.00	477.72
368.15	120.00	481.49
373.15	120.00	485.26
378.15	120.00	489.03
383.15	120.00	492.80
388.15	120.00	496.76
393.15	120.00	500.14
398.15	120.00	504.50
403.15	120.00	508.27
408.15	120.00	512.44
413.15	120.00	515.81
418.15	120.00	519.58
423.15	120.00	523.35
428.15	120.00	527.12
433.15	120.00	530.89
438.15	120.00	535.25
443.15	120.00	539.81
448.15	120.00	543.58
453.15	120.00	547.95
458.15	120.00	554.10
463.15	120.00	559.65
323.15	10120.00	447.76
328.15	10120.00	451.13
333.15	10120.00	454.51
338.15	10120.00	457.88
343.15	10120.00	461.25
348.15	10120.00	464.82
353.15	10120.00	468.20
358.15	10120.00	471.97
363.15	10120.00	475.54
368.15	10120.00	478.91
373.15	10120.00	483.07
378.15	10120.00	486.45
383.15	10120.00	489.82
388.15	10120.00	493.19
393.15	10120.00	497.16
398.15	10120.00	500.73
403.15	10120.00	503.71
408.15	10120.00	508.47
413.15	10120.00	511.64
418.15	10120.00	515.41
423.15	10120.00	518.78
428.15	10120.00	522.16
433.15	10120.00	525.93
438.15	10120.00	529.30
443.15	10120.00	533.47
448.15	10120.00	537.63
453.15	10120.00	541.60
458.15	10120.00	545.77
463.15	10120.00	550.33
468.15	10120.00	553.90
473.15	10120.00	558.07
478.15	10120.00	562.83
483.15	10120.00	566.79
Reference

Viscosity, Pa*s

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Viscosity, Pa*s - Liquid
313.20	690.00	0.0017
313.20	5000.00	0.0017
313.20	10000.00	0.0018
313.20	20000.00	0.0020
313.20	30000.00	0.0022
313.20	40000.00	0.0025
313.20	50000.00	0.0028
313.20	60000.00	0.0031
333.20	690.00	0.0012
333.20	5000.00	0.0013
333.20	10000.00	0.0013
333.20	20000.00	0.0015
333.20	30000.00	0.0016
333.20	40000.00	0.0017
333.20	50000.00	0.0019
333.20	60000.00	0.0020
353.20	690.00	0.0009
353.20	5000.00	0.0010
353.20	10000.00	0.0010
353.20	20000.00	0.0011
353.20	30000.00	0.0012
353.20	40000.00	0.0013
353.20	50000.00	0.0014
353.20	60000.00	0.0015
373.20	690.00	0.0007
373.20	5000.00	0.0007
373.20	10000.00	0.0008
373.20	20000.00	0.0009
373.20	30000.00	0.0009
373.20	40000.00	0.0010
373.20	50000.00	0.0011
373.20	60000.00	0.0012
393.20	690.00	0.0005
393.20	5000.00	0.0006
393.20	10000.00	0.0006
393.20	20000.00	0.0007
393.20	30000.00	0.0008
393.20	40000.00	0.0008
393.20	50000.00	0.0009
393.20	60000.00	0.0010
Reference

Mass density, kg/m3

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Mass density, kg/m3 - Liquid
294.80	2050.00	760.0
294.80	3540.00	762.0
294.40	5030.00	764.0
294.80	6500.00	765.0
294.60	8000.00	766.0
294.60	9490.00	767.0
324.10	2070.00	742.0
324.00	3540.00	743.0
324.00	5050.00	744.0
324.00	6560.00	746.0
324.10	8070.00	747.0
324.10	9540.00	748.0
373.50	2100.00	708.0
373.50	3560.00	709.0
373.30	5060.00	711.0
373.30	6560.00	712.0
373.50	8030.00	713.0
373.50	9500.00	715.0
447.60	1990.00	655.0
447.60	3590.00	658.0
447.50	4920.00	660.0
447.50	6450.00	662.0
447.60	7960.00	665.0
447.60	9470.00	667.0
Reference

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Mass density, kg/m3 - Liquid
283.15	100.00	770.0
283.15	470.00	770.2
283.15	960.00	770.5
298.15	100.00	759.4
298.15	470.00	759.7
298.15	960.00	760.0
298.15	2460.00	761.0
298.15	2950.00	761.3
298.15	4930.00	762.6
298.15	7410.00	764.2
298.15	9890.00	765.8
298.15	14850.00	768.9
298.15	19810.00	771.9
298.15	24770.00	774.8
298.15	29730.00	777.6
298.15	34690.00	780.3
298.15	39650.00	782.9
298.15	44610.00	785.4
298.15	49570.00	787.9
298.15	54530.00	790.3
298.15	59490.00	792.6
298.15	64450.00	794.9
298.15	69410.00	797.1
338.15	100.00	731.4
338.15	470.00	731.7
338.15	960.00	732.1
338.15	2460.00	733.3
338.15	2950.00	733.7
338.15	4930.00	735.3
338.15	7410.00	737.3
338.15	9890.00	739.2
338.15	14850.00	743.0
338.15	19810.00	746.5
338.15	29730.00	753.2
338.15	34690.00	756.4
338.15	39650.00	759.4
338.15	44610.00	762.4
338.15	49570.00	765.2
338.15	59490.00	770.7
338.15	64450.00	773.3
338.15	69410.00	775.8
338.15	44610.00	762.3
338.15	49570.00	765.1
338.15	54530.00	767.9
338.15	59490.00	770.6
338.15	64450.00	773.2
338.15	69410.00	775.7
288.15	100.00	766.4
288.15	470.00	766.7
288.15	960.00	766.9
288.15	2460.00	767.9
288.15	2950.00	768.2
288.15	4930.00	769.5
288.15	7410.00	771.0
288.15	9890.00	772.5
308.15	100.00	752.3
308.15	470.00	752.6
308.15	2460.00	754.0
308.15	4930.00	755.7
308.15	9890.00	759.1
308.15	14850.00	762.3
308.15	19810.00	765.4
308.15	24770.00	768.4
308.15	29730.00	771.3
308.15	34690.00	774.1
308.15	39650.00	776.9
308.15	44610.00	779.5
308.15	49570.00	782.1
308.15	54530.00	784.5
308.15	59490.00	787.0
308.15	64450.00	789.3
308.15	69410.00	791.6
358.15	100.00	717.2
358.15	470.00	717.5
358.15	960.00	718.0
358.15	2460.00	719.4
358.15	2950.00	719.8
358.15	4930.00	721.6
358.15	7410.00	723.8
358.15	9890.00	725.9
358.15	14850.00	730.0
358.15	19810.00	733.9
358.15	24770.00	737.6
358.15	29730.00	741.2
358.15	34690.00	744.6
358.15	39650.00	747.8
358.15	44610.00	751.0
358.15	49570.00	754.0
358.15	54530.00	757.0
358.15	59490.00	759.8
358.15	64450.00	762.5
358.15	69410.00	765.2
293.15	100.00	762.9
293.15	470.00	763.2
293.15	960.00	763.5
293.15	2460.00	764.5
293.15	2950.00	764.8
293.15	4930.00	766.0
293.15	7410.00	767.6
293.15	9890.00	769.2
318.15	100.00	745.4
318.15	470.00	745.6
318.15	960.00	746.0
318.15	2460.00	747.1
318.15	2950.00	747.4
318.15	4930.00	748.9
318.15	7410.00	750.7
318.15	9890.00	752.4
318.15	14850.00	755.8
318.15	19810.00	759.1
318.15	24770.00	762.3
318.15	29730.00	765.2
318.15	34690.00	768.2
318.15	39650.00	771.0
318.15	44610.00	773.8
318.15	49570.00	776.4
318.15	54530.00	779.0
318.15	59490.00	781.5
318.15	64450.00	784.0
318.15	69410.00	786.3
373.15	100.00	706.5
373.15	470.00	706.8
373.15	960.00	707.3
373.15	2460.00	708.8
373.15	2950.00	709.3
373.15	4930.00	711.3
373.15	7410.00	713.6
373.15	9890.00	715.9
373.15	14850.00	720.3
373.15	19810.00	724.5
373.15	24770.00	728.5
373.15	29730.00	732.2
373.15	34690.00	735.8
373.15	39650.00	739.3
373.15	44610.00	742.6
373.15	49570.00	745.7
373.15	54530.00	748.8
373.15	59490.00	751.8
373.15	64450.00	754.6
373.15	69410.00	757.4
Reference

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Mass density, kg/m3 - Liquid
313.19	10020.00	756.25
313.23	12040.00	757.62
313.15	14050.00	759.03
313.13	16040.00	760.35
313.15	18060.00	761.65
313.17	19040.00	762.28
323.26	10000.00	749.44
323.18	12040.00	750.93
323.14	14050.00	752.38
323.18	16070.00	753.74
323.23	18060.00	755.07
323.25	19080.00	755.76
333.14	10050.00	742.64
333.16	12040.00	744.14
333.28	14060.00	745.66
333.16	16060.00	747.18
333.13	18050.00	748.61
333.13	19060.00	749.31
343.32	10040.00	736.0
343.32	12050.00	737.59
343.35	14070.00	739.16
343.31	16030.00	740.68
343.34	18020.00	742.16
343.31	19040.00	742.92
353.63	10020.00	729.05
353.58	12050.00	730.83
353.66	14040.00	732.42
353.48	16030.00	734.17
353.50	18010.00	735.7
353.51	19050.00	736.41
Reference

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Mass density, kg/m3 - Liquid
323.20	1050.00	737.0
323.20	2020.00	742.0
323.20	3160.00	743.0
323.20	4070.00	744.0
323.20	5060.00	745.0
323.30	5940.00	745.0
373.40	2080.00	707.0
373.40	4050.00	709.0
373.40	6010.00	710.0
373.40	7070.00	711.0
373.50	2970.00	708.0
373.50	5010.00	710.0
373.60	1010.00	706.0
422.50	1080.00	672.0
422.50	2140.00	673.0
422.60	3020.00	675.0
422.60	4020.00	676.0
422.60	5040.00	677.0
422.60	6050.00	679.0
422.70	7000.00	680.0
422.70	8000.00	681.0
Reference

Fixed		Measured
Pressure, kPa - Liquid	Temperature, K - Liquid	Mass density, kg/m3 - Liquid
100.00	283.15	770.4
100.00	288.15	767.0
100.00	293.15	763.5
100.00	298.15	759.8
100.00	303.15	756.3
100.00	308.15	752.7
100.00	313.15	749.2
100.00	318.15	745.7
100.00	323.15	742.2
10000.00	283.15	776.4
10000.00	288.15	772.9
10000.00	293.15	769.6
10000.00	298.15	766.2
10000.00	303.15	762.8
10000.00	308.15	759.4
10000.00	313.15	756.0
10000.00	318.15	752.7
10000.00	323.15	749.4
20000.00	288.15	778.8
20000.00	293.15	775.6
20000.00	298.15	772.3
20000.00	303.15	769.0
20000.00	308.15	765.8
20000.00	313.15	762.5
20000.00	318.15	759.3
20000.00	323.15	756.2
30000.00	288.15	784.2
30000.00	293.15	781.1
30000.00	298.15	778.0
30000.00	303.15	774.8
30000.00	308.15	771.6
30000.00	313.15	768.5
30000.00	318.15	765.5
30000.00	323.15	762.4
40000.00	288.15	789.4
40000.00	293.15	786.4
40000.00	298.15	783.3
40000.00	303.15	780.2
40000.00	308.15	777.2
40000.00	313.15	774.2
40000.00	318.15	771.2
40000.00	323.15	768.4
50000.00	293.15	791.4
50000.00	298.15	788.4
50000.00	303.15	785.4
50000.00	308.15	782.4
50000.00	313.15	779.5
50000.00	318.15	776.6
50000.00	323.15	773.8
60000.00	293.15	796.1
60000.00	298.15	793.2
60000.00	303.15	790.3
60000.00	308.15	787.3
60000.00	313.15	784.5
60000.00	318.15	781.7
60000.00	323.15	779.0
Reference

Correlations

Property	Value	Unit	Temperature (K)	Source
Cp,gas	[246.43; 863.82]	J/mol×K	[200.00; 1500.00]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A + exp(B/T + C + D·T + E·T²) Y is Cp,gas in J/mol×K, T in K
Coefficient A			2.04940e+02
Coefficient B			-6.57010e+02
Coefficient C			7.03524e+00
Coefficient D			-1.32480e-04
Coefficient E			4.09020e-08
Temperature range, min.			200.00
Temperature range, max.			1500.00
Cp,gas	246.43	J/mol×K	200.00	Calculated Property
Cp,gas	366.85	J/mol×K	344.44	Calculated Property
Cp,gas	485.38	J/mol×K	488.89	Calculated Property
Cp,gas	581.23	J/mol×K	633.33	Calculated Property
Cp,gas	656.28	J/mol×K	777.78	Calculated Property
Cp,gas	715.46	J/mol×K	922.22	Calculated Property
Cp,gas	763.03	J/mol×K	1066.67	Calculated Property
Cp,gas	802.17	J/mol×K	1211.11	Calculated Property
Cp,gas	835.20	J/mol×K	1355.56	Calculated Property
Cp,gas	863.82	J/mol×K	1500.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
Cp,liquid	[429.47; 607.10]	J/mol×K	[279.01; 526.73]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A + exp(B/T + C + D·T + E·T²) Y is Cp,liquid in J/mol×K, T in K
Coefficient A			8.42570e+01
Coefficient B			1.10320e+02
Coefficient C			4.59924e+00
Coefficient D			3.37230e-03
Coefficient E			-1.17390e-06
Temperature range, min.			279.01
Temperature range, max.			526.73
Cp,liquid	429.47	J/mol×K	279.01	Calculated Property
Cp,liquid	442.98	J/mol×K	306.53	Calculated Property
Cp,liquid	458.55	J/mol×K	334.06	Calculated Property
Cp,liquid	475.86	J/mol×K	361.58	Calculated Property
Cp,liquid	494.69	J/mol×K	389.11	Calculated Property
Cp,liquid	514.90	J/mol×K	416.63	Calculated Property
Cp,liquid	536.34	J/mol×K	444.16	Calculated Property
Cp,liquid	558.92	J/mol×K	471.68	Calculated Property
Cp,liquid	582.54	J/mol×K	499.21	Calculated Property
Cp,liquid	607.10	J/mol×K	526.73	Calculated Property

Property	Value	Unit	Temperature (K)	Source
η	[0.0033348; 0.0000573]	Pa×s	[277.65; 693.00]	ChemSep v8.3 pure component data Compiled value
Equation			Y = exp(A + B/T + C·ln(T) + D·T^E) Y is η in Pa×s, T in K
Coefficient A			-8.46145e+01
Coefficient B			4.56743e+03
Coefficient C			1.12543e+01
Coefficient D			-1.11579e-05
Coefficient E			2.00000e+00
Temperature range, min.			277.65
Temperature range, max.			693.00
η	0.0033348	Pa×s	277.65	Calculated Property
η	0.0013240	Pa×s	323.80	Calculated Property
η	0.0007141	Pa×s	369.95	Calculated Property
η	0.0004549	Pa×s	416.10	Calculated Property
η	0.0003159	Pa×s	462.25	Calculated Property
η	0.0002281	Pa×s	508.40	Calculated Property
η	0.0001661	Pa×s	554.55	Calculated Property
η	0.0001197	Pa×s	600.70	Calculated Property
η	0.0000842	Pa×s	646.85	Calculated Property
η	0.0000573	Pa×s	693.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
ΔvapH	[73.01; 0.00]	kJ/mol	[279.01; 693.00]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A·(1 − Tr)^(B + C·Tr + D·Tr² + E·Tr³), Tr = T/Tc Y is ΔvapH in kJ/mol, T in K
Coefficient A			1.21637e+02
Coefficient B			1.28014e+00
Coefficient C			-3.52636e-01
Coefficient D			-1.24174e+00
Coefficient E			8.26459e-01
Critical temperature, Tc (K)			6.93000e+02
Temperature range, min.			279.01
Temperature range, max.			693.00
ΔvapH	73.01	kJ/mol	279.01	Calculated Property
ΔvapH	67.65	kJ/mol	325.01	Calculated Property
ΔvapH	62.81	kJ/mol	371.01	Calculated Property
ΔvapH	58.32	kJ/mol	417.01	Calculated Property
ΔvapH	53.97	kJ/mol	463.01	Calculated Property
ΔvapH	49.45	kJ/mol	509.00	Calculated Property
ΔvapH	44.31	kJ/mol	555.00	Calculated Property
ΔvapH	37.75	kJ/mol	601.00	Calculated Property
ΔvapH	28.03	kJ/mol	647.00	Calculated Property
ΔvapH	0.00	kJ/mol	693.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
Pvap	[1.33; 202.64]	kPa	[395.44; 554.00]	The Yaws Handbook of Vapor Pressure
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
Coefficient A			1.50005e+01
Coefficient B			-4.49932e+03
Coefficient C			-8.96310e+01
Temperature range, min.			395.44
Temperature range, max.			554.00
Pvap	1.33	kPa	395.44	Calculated Property
Pvap	2.97	kPa	413.06	Calculated Property
Pvap	6.10	kPa	430.68	Calculated Property
Pvap	11.66	kPa	448.29	Calculated Property
Pvap	20.97	kPa	465.91	Calculated Property
Pvap	35.80	kPa	483.53	Calculated Property
Pvap	58.38	kPa	501.15	Calculated Property
Pvap	91.46	kPa	518.76	Calculated Property
Pvap	138.29	kPa	536.38	Calculated Property
Pvap	202.64	kPa	554.00	Calculated Property
Pvap	[2.55e-04; 1599.81]	kPa	[279.01; 693.00]	ChemSep v8.3 pure component data Compiled value
Equation			Y = exp(A + B/T + C·ln(T) + D·T^E) Y is Pvap in kPa, T in K
Coefficient A			1.34862e+02
Coefficient B			-1.32657e+04
Coefficient C			-1.70704e+01
Coefficient D			6.90525e-06
Coefficient E			2.00000e+00
Temperature range, min.			279.01
Temperature range, max.			693.00
Pvap	2.55e-04	kPa	279.01	Calculated Property
Pvap	0.02	kPa	325.01	Calculated Property
Pvap	0.39	kPa	371.01	Calculated Property
Pvap	3.54	kPa	417.01	Calculated Property
Pvap	18.49	kPa	463.01	Calculated Property
Pvap	66.57	kPa	509.00	Calculated Property
Pvap	184.83	kPa	555.00	Calculated Property
Pvap	426.99	kPa	601.00	Calculated Property
Pvap	865.67	kPa	647.00	Calculated Property
Pvap	1599.81	kPa	693.00	Calculated Property
Pvap	[1.87e-04; 1663.13]	kPa	[279.01; 692.40]	KDB Vapor Pressure Data
Equation			ln(Y) = A + B/T + C·ln(T) + D·T² + E/T² Y is Pvap in kPa, T in K
Coefficient A			1.87822e+02
Coefficient B			-1.58065e+04
Coefficient C			-2.49854e+01
Coefficient D			1.21628e-05
Coefficient E			0.00000e+00
Temperature range, min.			279.01
Temperature range, max.			692.40
Pvap	1.87e-04	kPa	279.01	Calculated Property
Pvap	0.02	kPa	324.94	Calculated Property
Pvap	0.39	kPa	370.87	Calculated Property
Pvap	3.62	kPa	416.81	Calculated Property
Pvap	18.71	kPa	462.74	Calculated Property
Pvap	66.12	kPa	508.67	Calculated Property
Pvap	181.09	kPa	554.60	Calculated Property
Pvap	418.29	kPa	600.54	Calculated Property
Pvap	863.93	kPa	646.47	Calculated Property
Pvap	1663.13	kPa	692.40	Calculated Property
Pvap	[5.51; 102.81]	kPa	[428.01; 527.31]	NIST
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
Coefficient A			1.41318e+01
Coefficient B			-4.00563e+03
Coefficient C			-1.05616e+02
Reference			Camin and Rossini, 1955
Temperature range, min.			428.01
Temperature range, max.			527.31
Pvap	5.51	kPa	428.01	Calculated Property
Pvap	8.32	kPa	439.04	Calculated Property
Pvap	12.22	kPa	450.08	Calculated Property
Pvap	17.53	kPa	461.11	Calculated Property
Pvap	24.61	kPa	472.14	Calculated Property
Pvap	33.87	kPa	483.18	Calculated Property
Pvap	45.78	kPa	494.21	Calculated Property
Pvap	60.85	kPa	505.24	Calculated Property
Pvap	79.65	kPa	516.28	Calculated Property
Pvap	102.81	kPa	527.31	Calculated Property

Property	Value	Unit	Temperature (K)	Source
ρl	[771.42; 220.17]	kg/m3	[279.01; 693.00]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A / B^(1 + (1 − T/C)^D) Y is ρl in kg/m3, T in K
Coefficient A			5.21701e+01
Coefficient B			2.36950e-01
Coefficient C			6.93000e+02
Coefficient D			2.68610e-01
Temperature range, min.			279.01
Temperature range, max.			693.00
ρl	771.42	kg/m3	279.01	Calculated Property
ρl	741.88	kg/m3	325.01	Calculated Property
ρl	710.80	kg/m3	371.01	Calculated Property
ρl	677.80	kg/m3	417.01	Calculated Property
ρl	642.34	kg/m3	463.01	Calculated Property
ρl	603.54	kg/m3	509.00	Calculated Property
ρl	559.94	kg/m3	555.00	Calculated Property
ρl	508.52	kg/m3	601.00	Calculated Property
ρl	441.11	kg/m3	647.00	Calculated Property
ρl	220.17	kg/m3	693.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
γ	[0.03; 0.01]	N/m	[278.65; 526.75]	Jasper (1972), surface tension of pure liquid compounds Compiled value
Equation			Y = A + B·T + C·T² + D·T³ + E·T⁴ Y is γ in N/m, T in K
Coefficient A			5.20367e-02
Coefficient B			-8.69000e-05
Coefficient C			0.00000e+00
Coefficient D			0.00000e+00
Coefficient E			0.00000e+00
Temperature range, min.			278.65
Temperature range, max.			526.75
γ	0.03	N/m	278.65	Calculated Property
γ	0.03	N/m	306.22	Calculated Property
γ	0.02	N/m	333.78	Calculated Property
γ	0.02	N/m	361.35	Calculated Property
γ	0.02	N/m	388.92	Calculated Property
γ	0.02	N/m	416.48	Calculated Property
γ	0.01	N/m	444.05	Calculated Property
γ	0.01	N/m	471.62	Calculated Property
γ	0.01	N/m	499.18	Calculated Property
γ	0.01	N/m	526.75	Calculated Property
γ	[0.03; 3.38e-06]	N/m	[279.01; 687.20]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A + exp(B/T + C + D·T + E·T²) Y is γ in N/m, T in K
Coefficient A			-4.42480e-03
Coefficient B			1.72780e+02
Coefficient C			-4.46930e+00
Coefficient D			3.71720e-03
Coefficient E			-7.95420e-06
Comment			Range stopped where the equation turns negative; ChemSep gives it to 693 K.
Temperature range, min.			279.01
Temperature range, max.			687.20
γ	0.03	N/m	279.01	Calculated Property
γ	0.02	N/m	324.36	Calculated Property
γ	0.02	N/m	369.72	Calculated Property
γ	0.02	N/m	415.07	Calculated Property
γ	0.01	N/m	460.43	Calculated Property
γ	0.01	N/m	505.78	Calculated Property
γ	0.01	N/m	551.14	Calculated Property
γ	0.00	N/m	596.49	Calculated Property
γ	0.00	N/m	641.85	Calculated Property
γ	3.38e-06	N/m	687.20	Calculated Property

Property	Value	Unit	Temperature (K)	Source
λgas	[0.01; 0.09]	W/m×K	[279.01; 1000.00]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A·T^B / (1 + C/T + D/T²) Y is λgas in W/m×K, T in K
Coefficient A			-1.22400e+02
Coefficient B			8.68140e-01
Coefficient C			-5.50210e+08
Coefficient D			-2.13470e+10
Temperature range, min.			279.01
Temperature range, max.			1000.00
λgas	0.01	W/m×K	279.01	Calculated Property
λgas	0.01	W/m×K	359.12	Calculated Property
λgas	0.02	W/m×K	439.23	Calculated Property
λgas	0.02	W/m×K	519.34	Calculated Property
λgas	0.03	W/m×K	599.45	Calculated Property
λgas	0.04	W/m×K	679.56	Calculated Property
λgas	0.05	W/m×K	759.67	Calculated Property
λgas	0.06	W/m×K	839.78	Calculated Property
λgas	0.07	W/m×K	919.89	Calculated Property
λgas	0.09	W/m×K	1000.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
λliquid	[0.14; 0.09]	W/m×K	[279.01; 526.73]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A + exp(B/T + C + D·T + E·T²) Y is λliquid in W/m×K, T in K
Coefficient A			3.91350e-02
Coefficient B			-2.08630e+02
Coefficient C			-6.64930e-02
Coefficient D			-5.84400e-03
Coefficient E			2.17110e-06
Temperature range, min.			279.01
Temperature range, max.			526.73
λliquid	0.14	W/m×K	279.01	Calculated Property
λliquid	0.14	W/m×K	306.53	Calculated Property
λliquid	0.13	W/m×K	334.06	Calculated Property
λliquid	0.12	W/m×K	361.58	Calculated Property
λliquid	0.12	W/m×K	389.11	Calculated Property
λliquid	0.11	W/m×K	416.63	Calculated Property
λliquid	0.11	W/m×K	444.16	Calculated Property
λliquid	0.10	W/m×K	471.68	Calculated Property
λliquid	0.10	W/m×K	499.21	Calculated Property
λliquid	0.09	W/m×K	526.73	Calculated Property

Similar Compounds

Find more compounds similar to Tetradecane.

Mixtures

• Hexadecane + Tetradecane
• Pentadecane + Tetradecane
• Tetradecane + Water + 1-(1-methyl-2-propoxyethoxy)-2-propanol
• Benzene + Tetradecane
• Acetophenone + Tetradecane
• Decane + Tetradecane
• Methane + Decane + Tetradecane
• Carbon dioxide + Tetradecane
• Carbon dioxide + Decane + Tetradecane
• Benzaldehyde + Tetradecane
• Ethanol + Tetradecane
• 2-Pyrrolidinone, 1-methyl- + Tetradecane
• 2-Pyrrolidinone, 1-methyl- + Benzene, propyl- + Tetradecane
• Carbon dioxide + 1-Decanol + Tetradecane
• Acetonitrile + Tetradecane
• Benzyl methyl ketone + Tetradecane
• Tetradecane + Methyl tetradecanoate
• 2-Pyrrolidinone, 1-methyl- + Benzene, pentyl- + Tetradecane
• Propane, 1-nitro- + Tetradecane
• Methane + Tetradecane

Find more mixtures with Tetradecane.

Sources

• KDB Vapor Pressure Data
• Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) ChEDL chemicals 1.5.2, from Bradley, J.-C.; Williams, A.; Lang, A. Jean-Claude Bradley Open Melting Point Dataset. Figshare, 2014 (CC0).
• Hankinson and Thomson (1979), COSTALD parameters ChEDL chemicals 1.5.2, from Hankinson, R. W.; Thomson, G. H. A New Correlation for Saturated Densities of Liquids and Their Mixtures. AIChE J. 1979, 25, 653-663.
• IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 2 ChEDL chemicals 1.5.2, from Ambrose, D.; Tsonopoulos, C. Vapor-Liquid Critical Properties of Elements and Compounds. 2. Normal Alkanes. J. Chem. Eng. Data 1995, 40, 531-546.
• Jasper (1972), surface tension of pure liquid compounds ChEDL chemicals 1.5.2, from Jasper, J. J. The Surface Tension of Pure Liquid Compounds. J. Phys. Chem. Ref. Data 1972, 1, 841-1010 (as transcribed in Lange's Handbook).
• Passut and Danner (1973), critical constants and acentric factors ChEDL chemicals 1.5.2, from Passut, C. A.; Danner, R. P. Acentric Factor. A Valuable Correlating Parameter for the Properties of Hydrocarbons. Ind. Eng. Chem. Process Des. Dev. 1973, 12, 365-368.
• PSRK revision IV (2005), critical constants and acentric factors of 1000 components ChEDL chemicals 1.5.2, from Horstmann, S.; Jabłoniec, A.; Krafczyk, J.; Fischer, K.; Gmehling, J. PSRK Group Contribution Equation of State: Comprehensive Revision and Extension IV, Including Critical Constants and α-Function Parameters for 1000 Components. Fluid Phase Equilib. 2005, 227, 157-164.
• Cheméo Relay (1.0)
• ChemSep v8.3 pure component data Converted from ChemSep v8.3 pure component data, H. Kooijman and R. Taylor (2021, 2022), Artistic License 2.0; see how the values differ.
• Crippen Method
• Liquid liquid equilibria for n-alkanes (C12, C14, C17) + propylbenzene +NMP mixtures at temperatures between 298 and 328K
• Liquid solid equilibria under high pressure of tetradecane + pentadecane and tetradecane + hexadecane binary systems
• Thermodynamic properties of mixtures containing ionic liquids Vapor pressures and activity coefficients of n-alcohols and benzene in binary mixtures with 1-methyl-3-butyl-imidazolium bis(trifluoromethyl-sulfonyl) imide
• Infinite dilution activity coefficients, specific retention volumes and solvation thermodynamics of hydrocarbons in C78H158 branched alkane solvent
• Solution thermodynamics near the liquid liquid critical point I. First-order excess derivatives
• Liquid viscosities of benzene, n-tetradecane, and benzene + n-tetradecane from 313 to 393K and pressures up to 60MPa: Experiment and modeling
• Determination and correlation of liquid-liquid equilibria for nine binary acetonitrile + n-alkane systems
• Separation of propylbenzene and n-alkanes from their mixtures using 4-methyl-N-butylpyridinium tetrafluoroborate as an ionic solvent at several temperatures
• Vapor liquid equilibrium measurement and thermodynamic modeling of binary systems (methane + n-tetradecane)
• Experimental and thermodynamic modeling study on (vapor + liquid) equilibria and physical properties of ternary systems (methane + n-decane + n-tetradecane)
• Measurement and correlation of saturated liquid properties and gas solubility for decane, tetradecane and their binary mixtures saturated with carbon dioxide
• Liquid-liquid equilibria for the ternary system (water + tetradecane + 1-methyl-2-propoxyethoxy-2-propanol)
• Liquid-liquid equilibria for benzaldehyde + n-alkane mixtures andcharacterization of benzaldehyde + hydrocarbon systems in terms of DISQUAC
• Experimental and theoretical study of interaction between organic compounds and 1- (4-sulfobutyl)-3-methylimidazolium based ionic liquids
• High-pressure densities and interfacial tensions of binary systems containing carbon dioxide + n-alkanes: (n-Dodecane, n-tridecane, n-tetradecane)
• Study of interaction between organic compounds and mono or dicationic oxygenated ionic liquids using gas chromatography
• Experimental measurements and thermodynamic modeling of wax disappearance temperature for the binary systems n-C14H30 + n- C16H34, n-C16H34 + n-C18H38 and n-C11H24 + n-C18H38
• Liquid liquid equilibria for acetophenone + n-alkane mixtures and characterization of acetophenone systems using DISQUAC
• Isobaric vapor-liquid equilibrium for the three binary systems of C14 - C16 n-alkane + methyl myristate at 5.00 kPa
• Thermodynamics of aromatic polar compound (alkanone, alkanal or alkanoate) + hydrocarbon mixtures
• Volume expansion prediction of supercritical CO 2 + crude oil
• Viscosity and density measurements on liquid n-tetradecane at moderately high pressures
• Solubility behavior of .gamma.-valerolactone + n-tetradecane or diesel mixtures at different temperatures
• CO2 and alkane minimum miscible pressure estimation by the extrapolation of interfacial tension
• Extraction of pentylbenzene from high molar mass alkanes (C14 and C17) by N-methyl-2-pyrrolidone
• Excess molar enthalpies of binary mixtures containing 2-decanone or dipentyl ether with long-chain n-alkanes at T = 298.15 K
• Interfacial tensions of binary mixtures of ethanol with octane, decane, dodecane, and tetradecane
• Evaluation of [bmim][PF6] as an ionic solvent for the extraction of propylbenzene from aliphatic compounds
• Thermodynamics of mixtures containing amines. XI. Liquid + liquid equilibria and molar excess enthalpies at 298.15 K for N-methylaniline + hydrocarbon systems. Characterization in terms of DISQUAC and ERAS models
• Phase composition and saturated liquid properties in binary and ternary systems containing carbon dioxide, n-decane, and n-tetradecane
• Activity coefficients at infinite dilution of organic solutes in methylphosphonate based ionic liquids using gas-liquid chromatography
• Measurement and correlation of solubility of carbon dioxide in triglycerides
• Super- and near-critical fluid phase behavior and phenomena of the ternary system CO2 + 1-decanol + n-tetradecane
• Heat capacity and Joule-Thomson coefficient of selected n-alkanes at 0.1 and 10 MPa in broad temperature ranges
• Determination of thermophysical properties of cyclopentane hydrate using a stirred calorimetric cell
• (p, n, T) Behavior of CO2 + Tetradecane Systems: Experiments and Thermodynamic Modeling
• Excess Molar Volumes for Three and Four Component Mixtures Simulating the Binary Mixture (Cyclohexane+ Hexadecane)
• Density, Viscosity, Speed of Sound, Bulk Modulus, Surface Tension, and Flash Point of Binary Mixtures of Butylbenzene + Linear Alkanes (n-Decane, n-Dodecane, n-Tetradecane, n-Hexadecane, or n-Heptadecane) at 0.1 MPa
• Liquid Liquid Equilibria for Systems Containing 4-Phenylbutan-2-one or Benzyl Ethanoate and Selected Alkanes
• Isothermal Vapor Pressures of Three Binary Systems: n-Tetradecane + Methyl Dodecanoate, Methyl Tetradecanoate, or Methyl Hexadecanoate between 353.15 and 453.15 K
• Interfacial Tension Measurement and Calculation of (Carbon Dioxide + n-Alkane) Binary Mixtures
• Measurement and Correlation of High Pressure Phase Equilibria for CO2 + Alkanes and CO2 + Crude Oil Systems
• Liquid-Liquid Equilibria for 2-Phenylethan-1-ol + Alkane Systems
• Effect of Solvent Cation Alkyl-Chain Length on the Separation of Butylbenzene from n-Tetradecane Using Hexafluorophosphate-Based Ionic Liquids at (313.15 and 333.15) K and 101.3 kPa
• Low-Pressure VLE Measurements and Thermodynamic Modeling, with PSRK and NRTL, of Binary 1-Alcohol + n-Alkane Systems
• Liquid-Liquid Equilibria for Ternary Mixtures of gamma-Valerolactone + n-Tetradecane + (Butanoic Acid or Hexanoic Acid or Methyl Myristate) at 298.15 K
• Measurement and Prediction of Excess Properties of Binary Mixtures Methyl Decanoate + an Even-Numbered n-Alkane (C6-C16) at 298.15 K
• Density, Viscosity, Refractive Index, and Speed of Sound in the Binary Mixtures of Tri-n-butylamine + Triethylamine, + Tetrahydrofuran, + Tetradecane, + Tetrachloroethylene, + Pyridine, or + Trichloroethylene at (298.15, 303.15, and 308.15) K
• Excess Enthalpies of Binary Mixtures of 1-Hexene with Some n-Alkanes at 298.15 K
• Thermodynamics of Mixtures Containing Ethers. Part III. Liquid-Liquid Equilibria for 2,5,8,11-Tetraoxadodecane or 2,5,8,11,14-Pentaoxapentadecane + Selected N-Alkanes
• Densities and Viscosities of Binary Mixtures of exo-Tetrahydrodicyclopentadiene with N-Undecane or N-Tetradecane at T = (293.15 to 313.15) K
• Activity Coefficients at Infinite Dilution of Organic Compounds in Four New Imidazolium-Based Ionic Liquids
• Liquid Liquid Equilibria of Alkane (C10 C14) + sec-Butylbenzene + Sulfolane
• Liquid Liquid Equilibria for the Ternary System Water + Tetradecane + Propylene Glycol n-Propyl Ether
• Measurement and Modeling of Liquid Saturated Properties (Solubility, Density, and Viscosity) of (Ethane + n-Tetradecane) Binary Systems
• Evaluation of the Performance of Trigeminal Tricationic Ionic Liquids for Separation Problems
• Thermodynamics of Mixtures Containing Aromatic Alcohols. 1. Liquid Liquid Equilibria for (Phenylmethanol + Alkane) Systems
• Isothermal Vapor Liquid Equilibria of n-Tetradecane + Ethyl Hexanoate, Ethyl Decanoate, and Ethyl Tetradecanoate
• Thermodynamics of Mixtures Containing a Very Strongly Polar Compound. 10. Liquid Liquid Equilibria for N,N-Dimethylacetamide + Selected Alkanes
• Excess Molar Volumes and Viscosities of Binary Systems of Butylcyclohexane with n-Alkanes (C7 to C14) at T = 293.15 K to 313.15 K
• Thermodynamics of Mixtures Containing Amines. XV. Liquid Liquid Equilibria for Benzylamine + CH3(CH2)nCH3 (n = 8, 9, 10, 12, 14)
• Liquid-Liquid Equilibria of Alkane (C10-C14) + Hexylbenzene + Sulfolane
• Solid-Liquid Equilibria of Dibenzothiophene and Dibenzothiophene Sulfone in Organic Solvents
• Infinite Dilution Binary Diffusion Coefficients of Hydrotreating Compounds in Tetradecane in the Temperature Range from (310 to 475) K
• Thermophysical Characterization of Liquids Using Precise Density and Isobaric Heat Capacity Measurements As a Function of Pressure
• Liquid Viscosities of Cyclohexane, Cyclohexane + Tetradecane, and Cyclohexane + Benzene from (313 to 393) K and Pressures Up to 60 MPa
• Liquid Viscosities of the Ternary System Benzene + Cyclohexane + n-Tetradecane from (313 to 393) K and Pressures up to 60 MPa
• Gas Saturation Vapor Pressure Measurements of Mononitrotoluene Isomers from (283.15 to 313.15) K
• Excess Molar Enthalpies of Binary Systems of 2-Octanone or 3-Octanone with Dodecane, Tetradecane, or Hexadecane at 298.15 K
• Partition Coefficients of Organic Compounds in New Imidazolium and Tetralkylammonium Based Ionic Liquids Using Inverse Gas Chromatography
• Excess Molar Enthalpies of Binary Systems of n-Valeric Anhydride or n-Hexanoic Anhydride with n-Dodecane, n-Tetradecane, or n-Hexadecane at 298.15 K
• Isobaric Thermal Expansivity for Nonpolar Compounds
• Study of Ether-, Alcohol-, or Cyano-Functionalized Ionic Liquids Using Inverse Gas Chromatography
• Joback Method
• KDB
• Aqueous Solubility Prediction Method
• Estimated Solubility Method
• McGowan Method
• NIST Webbook
• The Yaws Handbook of Vapor Pressure

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